Fluidized bed device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene

Patent metadata

Field	Value
Publication number	US-11161085-B2
Application number	US-201716608422-A
Country	US
Kind code	B2
Filing date	Nov 24, 2017
Priority date	Apr 27, 2017
Publication date	Nov 2, 2021
Grant date	Nov 2, 2021

Abstract

A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors; the first reactor feed distributor and the plurality of second reactor feed distributions are sequentially arranged.

First claim

What is claimed is:

1. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, wherein the turbulent fluidized bed reactor comprising a reaction zone, a dilute phase zone, a first reactor feed distributor and a plurality of second reactor feed distributors, the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged from bottom to top in the reaction zone; wherein the reaction zone is located in a lower part of the turbulent fluidized bed reactor; and the dilute phase zone is located in an upper part of the turbulent fluidized reactor bed;
the number of the second reactor feed distributors is in a range from 2 to 10;
wherein the turbulent fluidized bed reactor further comprises a first reactor gas-solid separator; the first reactor gas-solid separator is placed in the dilute phase zone or outside a reactor shell, the first reactor gas-solid separator is provided with a regenerated catalyst inlet, a catalyst outlet of the first reactor gas-solid separator is placed at the bottom of a reaction zone, and a gas outlet of the first reactor gas-solid separator is placed in the dilute phase zone.

2. The turbulent fluidized bed reactor of claim 1 , the turbulent fluidized bed reactor further comprises a second reactor gas-solid separator, the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor shell;
an inlet of the second reactor gas-solid separator is placed in the dilute phase zone, a catalyst outlet of the second reactor gas-solid separator is placed in the reaction zone, and a gas outlet of the second reactor gas-solid separator is connected to a product gas outlet of the turbulent fluidized bed reactor;
the first reactor gas-solid separator and the second reactor gas-solid separator are cyclone separators.

3. The turbulent fluidized bed reactor of claim 1 , the turbulent fluidized bed reactor further comprises a reactor heat extractor, and the reactor heat extractor is arranged inside or outside the shell of the turbulent fluidized bed reactor;
preferably, the reactor heat extractor is arranged between the plurality of reactor feed distributors.

4. The turbulent fluidized bed reactor of claim 1 , the turbulent fluidized bed reactor further comprises a reactor stripper, the reactor stripper passes through the reactor shell from the outside to the inside at the bottom of the turbulent fluidized bed reactor and is opened in the reaction zone of the turbulent fluidized bed reactor, and a reactor stripping gas inlet and a spent catalyst outlet are arranged at the bottom of the reactor stripper.

5. The turbulent fluidized bed reactor of claim 1 , the turbulent fluidized bed reactor further comprises a perforated plate located between the first reactor feed distributor and at least one of the second reactor feed distributors, the porosity of the perforated plate is less than or equal to 50%;
preferably, the turbulent fluidized bed reactor comprises a perforated plate located between the first reactor feed distributor and the second reactor feed distributor closest to the first reactor feed distributor, the porosity of the perforated plate is in a range from 5% to 50%.

6. The turbulent fluidized bed reactor of claim 1 , wherein the reactor stripper passes through the reactor shell from the outside to the inside at the bottom of the turbulent fluidized bed reactor and is opened in the reaction zone of the turbulent fluidized bed reactor, and a reactor stripping gas inlet and a spent catalyst outlet are arranged at the bottom of the reactor stripper;
the turbulent fluidized bed reactor comprises a perforated plate located between the first reactor feed distributor and the second reactor feed distributor closest to the first reactor feed distributor, the porosity of the perforated plate is in a range from 5% to 50%;
the horizontal height of opening of the reactor stripper in the reactor shell is higher than that of the first reactor feed distributor and higher than that of the perforated plate.

7. A device for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, wherein the device comprises a turbulent fluidized bed reactor and a fluidized bed regenerator for regenerating a catalyst, wherein the turbulent fluidized bed reactor comprises a reaction zone, a dilute phase zone, a first reactor feed distributor and a plurality of second reactor feed distributors, the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged from bottom to top in the reaction zone; wherein the reaction zone is located in a lower part of the turbulent fluidized bed reactor, and the dilute phase zone is located in an upper part of the turbulent fluidized bed reactor;
the number of the second reactor feed distributors is in a range from 2 to 10;
wherein the turbulent fluidized bed reactor comprises a first reactor gas-solid separator, the first reactor gas-solid separator is placed in the dilute phase zone or outside a reactor shell, the first reactor gas-solid separator is provided with a regenerated catalyst inlet, a catalyst outlet of the first reactor gas-solid separator is placed at the bottom of a reaction zone, and a gas outlet of the first reactor gas-solid separator is placed in the dilute phase zone.

8. The device of claim 7 , wherein the fluidized bed regenerator is a turbulent fluidized bed regenerator, and the fluidized bed regenerator comprises a regenerator shell, a regenerator gas-solid separator, a regenerator heat extractor and the regenerator stripper; the lower part of the fluidized bed regenerator is a regeneration zone, the upper part of the fluidized bed regenerator is a dilute phase zone of the regenerator, the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, and the regenerator gas-solid separator is placed in the dilute phase zone or outside the regenerator shell; and
the inlet of the regenerator gas-solid separator is placed in the dilute phase zone of the regenerator, the catalyst outlet of the regenerator gas-solid separator is placed in the regeneration zone, and the regenerator stripper is opened at the bottom of the regenerator shell.

9. The device of claim 7 , the fluidized bed regenerator further comprises a regenerator shell, a regenerator feed distributor, a regenerator gas-solid separator, a regenerator heat extractor, a flue gas outlet and a regenerator stripper;
the lower part of the fluidized bed regenerator is a regeneration zone, and the upper part of the fluidized bed regenerator is a dilute phase zone;
the regenerator feed distributor is placed at the bottom of the regeneration zone, the regenerator heat extractor is placed in the regeneration zone, the regenerator gas-solid separator is placed in the dilute phase zone or outside the regenerator shell, the inlet of the regenerator gas-solid separator is placed in the dilute phase zone, the catalyst outlet of the regenerator gas-solid separator is placed in the regeneration zone, the gas outlet of the regenerator gas-solid separator is connected to the flue gas outlet, and the regenerator stripper is opened at the bottom of the regenerator shell;
the spent catalyst outlet of the reactor stripper is connected to the inlet of an inclined spent catalyst pipe, a spent catalyst sliding valve is arranged in the inclined spent catalyst pipe, the outlet of the inclined spent catalyst pipe is connected to the inlet of a spent catalyst lift pipe, the bottom of the spent catalyst lift pipe is provided with a spent catalyst

Assignees

• Dalian Inst Chem & Physics Cas

Inventors

• Zhang Tao
• Ye Mao
• Liu Zhongmin
• Zhang Jinling
• Tang Hailong
• Jia Jinming
• He Changqing
• Wang Xiangao
• Zhang Cheng
• Li Hua
• Zhao Yinfeng
• Li Chenggong

Classifications

• Y02P30/40

  Ethylene production · CPC title

• Y02P30/20

  using bio-feedstock · CPC title

• B01J8/18 Primary

  with fluidised particles {(combustion apparatus with fluidised bed in general F23C10/00; furnaces with fluidised bed F27B15/00)} · CPC title

• Y02P20/584

  Recycling of catalysts · CPC title

• Y02P20/52

  using catalysts, e.g. selective catalysts · CPC title